EP0177806B1 - Process for the desulphurization of fumes - Google Patents

Process for the desulphurization of fumes Download PDF

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Publication number
EP0177806B1
EP0177806B1 EP85111668A EP85111668A EP0177806B1 EP 0177806 B1 EP0177806 B1 EP 0177806B1 EP 85111668 A EP85111668 A EP 85111668A EP 85111668 A EP85111668 A EP 85111668A EP 0177806 B1 EP0177806 B1 EP 0177806B1
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EP
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Prior art keywords
sulfuric acid
evaporation
sulphuric acid
gas
scrubber
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EP85111668A
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German (de)
French (fr)
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EP0177806A2 (en
EP0177806A3 (en
Inventor
Günter Dr. Lailach
Rudolf Dr. Gerken
Karl-Heinz Dr. Schultz
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Kerr-Mcgee Pigments & Co KG GmbH
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Bayer AG
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8609—Sulfur oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • C01B17/775—Liquid phase contacting processes or wet catalysis processes

Definitions

  • the present invention relates to a process for the desulfurization of S0 2 and hydrogen halide flue gases by catalytic oxidation of the sulfur dioxide on moist activated carbon at temperatures of 45 to 70 ° C with the formation of 3 to 20% dilute sulfuric acid.
  • Chemical Abstracts 89: 30195x describes a process for cleaning gases containing sulfur dioxide, which also contain halogen compounds as constituents. These halogen compounds are removed here by separate evaporation of the acid in vacuo.
  • the aim of the present invention is to provide an economical, simple apparatus and reliable method for desulfurization of flue gases which does not have the disadvantages of the known methods.
  • This goal is achieved by a process in which the SO Z -containing flue gas emitted from the power plant before the oxidation at the activated carbon contact of a laundry (1) with a 50-85% sulfuric acid and a laundry (11) with a 5- to Is subjected to 25% sulfuric acid.
  • the present invention thus relates to a process for the desulfurization of SO Z and hydrogen halide flue gases by catalytic oxidation of the sulfur dioxide on moist activated carbon at temperatures from 45 to 70 ° C. with the formation of 3 to 20% dilute sulfuric acid, which is characterized in that the diluted sulfuric acid is evaporated by contact with the hot flue gases to be desulfurized in two stages in cocurrent or countercurrent heat exchangers to a sulfuric acid concentration of 60 to 85% and in the dilute sulfuric acid dissolved hydrochloric and hydrofluoric acids by evaporation from a mixture of the dilute sulfuric acid from the second stage Washer with the concentrated sulfuric acid from the first stage of the washer, the mixture having an H 2 S0 4 concentration of 40 to 70%.
  • the flue gases are cooled down to 90 to 110 ° C.
  • a second wash (11) is then carried out with 5 to 25% sulfuric acid, in which the HCI and HF are absorbed in the acid. This avoids negative influences on the catalytic conversion of S0 2 on the activated carbon.
  • the approximately 45 to 70 ° C hot, largely dust-free flue gas is passed through an activated carbon layer, which is continuously or intermittently sprayed with so much water that a 3 to 20% sulfuric acid flows off.
  • the gas stream can alternatively be passed through the coal layer from bottom to top or vice versa.
  • the flue gas When flowing through the activated carbon layer, the flue gas is saturated with water vapor and cooled to 45 to 55 ° C. This cooling can be avoided if water vapor is introduced into the flue gas before entering the activated carbon layer, preferably after washing (1), e.g. evaporation occurs in various processes.
  • the 3 to 20% sulfuric acid obtained in the activated carbon reactor during desulfurization is almost worthless.
  • this acid is ultimately fed via the sulfuric acid cycle of the laundry (11) into the sulfuric acid cycle of the laundry (I), in which so much water is released to the flue gas by evaporative cooling that a 60 to 85% strength sulfuric acid is fed out.
  • This acid can either be used directly, for example in the fertilizer industry, or can be evaporated to an H 2 S0 4 content of 80 to 93% using known methods with relatively little effort.
  • the advantage here is that HCI and HF are largely removed from the flue gas by adsorption in the 5 to 25% sulfuric acid before it is introduced into the activated carbon reactor, and that when the flue gas cools from 90 to 110 ° C 45 to 70 ° C released gas heat is used for acid evaporation.
  • the HCI and HF are expelled from the washing acid of the washing circuit (11) by mixing the HCI and HF-containing 5 to 25% sulfuric acid fed out of the washing (11) with as much 60 to 85% sulfuric acid from the Wash (1) that a 40-70% sulfuric acid results. From this sulfuric acid, HCI, HF and part of the water are evaporated by stripping with air or flue gas or by evacuation. The vapors can be condensed by indirect or direct cooling.
  • the removal of hydrogen chloride and hydrogen fluoride is carried out by vacuum evaporation from a mixture of the dilute sulfuric acid from the second stage of the scrubber with the concentrated sulfuric acid from the first stage of the scrubber, the mixture having an H 2 SO 4 concentration from 40 to 70%.
  • the embodiment in which the removal of hydrogen chloride and hydrogen fluoride from a mixture of the dilute sulfuric acid from the second stage of the scrubber with the concentrated sulfuric acid from the first stage of the scrubber can be just as advantageous, the mixture being an H 2 SO 4 - Has a concentration of 40 to 70%, by blowing out with air or flue gas and then washing out the hydrogen halide from the gas with water.
  • the condensation of the vapors can advantageously be achieved by direct cooling and washing with cooling water.
  • a flue gas desulfurization system is shown here for total current desulfurization with a clean gas S0 2 content below 400 mg / m n , consisting of a gas scrubber (I), in which flue gas cooling and humidification, fine dust removal and sulfuric acid concentration takes place, gas scrubbing (11) , in which the further gas cooling with simultaneous sulfuric acid concentration as well as the fine dust removal and the HCI and HF removal from the flue gas takes place, an activated carbon reactor (5) for the catalytic conversion of the sulfur dioxide with oxygen and water to sulfuric acid and an auxiliary system (7, 8) Removal of HCI and HF from sulfuric acid.
  • the flue gas (10) is conveyed through the scrubber (1) by means of the fan (9), in which it is cooled to 90 to 110 ° C. by contact with 50 to 85% sulfuric acid.
  • the gas (11) emerging from the scrubber (1) is contacted in the scrubber (3) with 5 to 25% sulfuric acid.
  • the gas is cooled to 50 to 70 ° C and the majority of the HCI and HF are adsorbed in the sulfuric acid.
  • the almost water vapor-saturated and largely dust-free flue gas (12) is passed in the reactor (5) through a moist activated carbon layer (6), in which sulfuric acid is formed from sulfur dioxide, oxygen and water.
  • the clean gas (13) emerging from the reactor (5) is passed into the atmosphere directly or after heating by means of hot flue gases or a partial flow of the raw gas or after indirect heating in heat exchangers.
  • the sulfuric acid formed in the activated carbon layer (6) of the reactor (5) is removed by continuously or discontinuously spraying the carbon layer (6) with water (27) as 3 to 20% sulfuric acid (14) and into the circulating acid (15) Laundry (11) fed.
  • water (27) as 3 to 20% sulfuric acid (14) and into the circulating acid (15) Laundry (11) fed.
  • 5 to 25% strength sulfuric acid (15) is drawn off from the bottom of the washer (3) by means of the pump (4) and essentially (16) conveyed into the head part of the washer.
  • a partial flow (17) which corresponds to the flow (14) minus the amount of water evaporated in the scrubber (3), is placed in a vacuum cooler together with 60- to 85% sulfuric acid (18) as 40-70% sulfuric acid (19) (7) fed. HCI, HF and a small amount of water evaporate in it.
  • the vapors (21) are condensed in an injection condenser (8) with cooling water (22) and discharged as weakly acidic waste water (23).
  • the HCl - and HF-free sulfuric acid (20) is fed into the acid cycle of the laundry (I). In this wash, the raw gas is washed with 60 to 85% sulfuric acid (25). After evaporation of part of the water from the acid, the 60 to 85% strength sulfuric acid (24) is drawn off from the bottom of the scrubber (1) by means of the circulation pump (2).
  • the 60 to 85% sulfuric acid (26) obtained as production can be cooled from 90 to 110 ° C by indirect cooling or fed to a further evaporation.
  • the gas scrubbing and the acid evaporation can also take place in washing towers, venturi scrubbers or similarly suitable apparatuses in cocurrent or countercurrent to the flue gas to the sulfuric acid fed in.
  • HCI and HF removal can also be carried out by blowing out the acid (19) with air or flue gas instead of in a vacuum cooler (7).
  • the HCI and HF-laden air or the flue gas must then be cleaned with water in a gas scrubber. If a possible use for the acids from the broth (21), these vapors are cooled indirectly.
  • the example relates to a flue gas desulfurization according to FIG. 1,210,000 m 3 n / h flue gas (10) with a content of 7.15% by volume H 2 0.6% by volume O 2 .
  • 3.3 SO 2 / m 3 n , 0.2 g HCl / m 3 n and 30 mg dust / m 3 n are introduced into the scrubber (1) at a temperature of 130 ° C.
  • Upon contact with 69% sulfuric acid (25) 3.06t H 2 0 / h is evaporated from this acid.
  • the flue gas (11) reaches the scrubber (3) at 100 ° C., where it is washed with 18.9% sulfuric acid (16).
  • the flue gas (12) emerging from the scrubber (3) at 53 ° C. contains 11.75% by volume H 2 O, 3.3 g SO 2 / m 3 n , less than 10 mg dust / m 3 n and traces of HCI.
  • the S0 2 content of the flue gas is reduced by catalytic oxidation to sulfuric acid from 3.3 g / m 3 n to 350 to 400 mg / m3 in the clean gas (13).
  • the sulfuric acid formed is washed out in the reactor (5) by periodically spraying the carbon layer with 9.75 m 3 / h of water (27) as 8.4% strength sulfuric acid (14).
  • This sulfuric acid is fed to the acid circuit of the washer (3).
  • 5.75t H 2 0 / h are evaporated from the sulfuric acid.
  • 4.63t / h of the 18.9% recycle acid (17), which also contain 0.84% HCl, are mixed with 7.15t / h 70% sulfuric acid (18) from the washer (1) and placed in the vacuum cooler ( 7) fed as 50% sulfuric acid at 80 ° C (19).
  • the HCI-free 51% sulfuric acid (20) from the vacuum cooler (7) is fed into the acid cycle of the laundry (I). From washer (1), 1.24 t / h of 70% sulfuric acid (26) are fed out at 100 ° C. as production.

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  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
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Abstract

In the desulphurizing of SO2- and hydrogen halide-containing flue gases by catalytically oxidizing the sulphur dioxide on moist active carbon at a temperature of from 45 DEG to 70 DEG C. with the formation of 3 to 20% dilute sulphuric acid, the improvement which comprises contacting the dilute sulphuric acid with the hot flue gases to be desulphurized so as to evaporate water resulting sulphuric acid of a concentration of from 60 to 85%, and removing by evaporation the hydrogen chloride and hydrogen fluoride dissolved in the dilute sulphuric acid. Advantageously evaporation is carried out in two scrubbing stages, the hydrogen chloride and hydrogen fluoride being removed, by vacuum evaporation or by stripping with air or flue gas, from a mixture of the dilute sulphuric acid from the second scrubbing stage with the concentrated sulphuric acid from the first scrubbing stage, the mixture having the H2SO4 concentration of from 40 to 70%.

Description

Die vorliegende Erfindung betrifft ein Verfahren zur Entschwefelung S02- und halogenwasserstoffhaltiger Rauchgase durch katalytische Oxidation des Schwefeldioxids an feuchter Aktivkohle bei Temperaturen von 45 bis 70°C unter Bildung von 3- bis 20%iger verdünnter Schwefelsäure.The present invention relates to a process for the desulfurization of S0 2 and hydrogen halide flue gases by catalytic oxidation of the sulfur dioxide on moist activated carbon at temperatures of 45 to 70 ° C with the formation of 3 to 20% dilute sulfuric acid.

Die Entschwefelung von Rauchgasen, insbesondere der grossen Rauchgasmengen, die bei der Verstromung von Kohle und schwerem Heizöl in Kraftwerken anfallen, ist eine aktuelle Forderung. Die bisher bekannten Verfahren sind mit erheblichem apparativen Aufwand verbunden. Die meisten Verfahren basieren auf der Umsetzung von Ca-Verbindungen, insbesondere gemahlenem Kalkstein, zu Gips. Der geringe Wert dieses Entproduktes, das infolge seines hohen Wassergehaltes einen erheblichen Aufwand für Lagerung, Entwässerung und Transport zu Deponien oder Verwendern erfordert, stellt keine merkliche wirtschaftliche Entlastung des Gesamtaufwandes dar.The desulphurization of flue gases, especially the large quantities of flue gas that arise from the generation of electricity from coal and heavy heating oil in power plants, is a current requirement. The previously known methods are associated with considerable expenditure on equipment. Most processes are based on the conversion of Ca compounds, especially ground limestone, to gypsum. The low value of this waste product, which due to its high water content requires considerable effort for storage, drainage and transport to landfills or users, does not represent a noticeable economic relief for the total effort.

Aus der DE-A-2 137 847 ist ein Verfahren und eine Vorrichtung zur Entschwefelung von Abgasen bekannt, bei dem ein Teil des Abgases über Aktivkohle zwecks Desorption des Schwefeldioxids geleistet wird. Die Temperatur der Aktivkohle liegt dabei bei über 100°C.From DE-A-2 137 847 a method and a device for the desulphurization of exhaust gases is known, in which a part of the exhaust gas is supplied via activated carbon for the purpose of desorbing the sulfur dioxide. The temperature of the activated carbon is over 100 ° C.

Weiter ist aus der GB-A-994 070 bekannt, die Entschwefelung von Prozessabgasen durch Oxidation des Schwefeldioxides in Gegenwart von Wasser zu Schwefelsäure an speziellen Aktivkohle-Katalysatoren durchzuführen. Das Verfahren, das als «Sulfacid-Verfahren» bekannt wurde, führt im allgemeinen zu einer 5- bis 20%igen Schwefelsäure. Die fehlenden Verbindungsmöglichkeiten für derart verdünnte Schwefelsäure sowie die Forderung, dass das 502-haltige in den Festbettreaktor eingeleitete Gas weniger als 20 mg Staub/m3 enthalten soll, führten dazu, dass dieses Verfahren bisher als mögliche Alternative für die obengenannten Verfahren der Rauchgasentschwefelung nicht berücksichtigt wurde.It is also known from GB-A-994 070 to carry out the desulphurization of process exhaust gases by oxidation of the sulfur dioxide in the presence of water to give sulfuric acid on special activated carbon catalysts. The process, known as the "sulfacid process", generally results in 5 to 20% sulfuric acid. The lack of connection options for such dilute sulfuric acid and the requirement that the 50 2 -containing gas introduced into the fixed bed reactor should contain less than 20 mg dust / m 3 did not result in this process being a possible alternative for the abovementioned processes for flue gas desulfurization taken into consideration.

Für die Entschwefelung von Rauchgasen mit einem relativ hohen Gehalt an HCI und HF sind darüber hinaus keine Verfahren bekannt.In addition, no processes are known for the desulfurization of flue gases with a relatively high content of HCI and HF.

Aus Chemical Abstracts 89: 30195x geht ein Verfahren zur Reinigung schwefeldioxid-enthaltender Gase hervor, die darüber hinaus auch Halogenverbindungen als Bestandteile enthalten. Die Entfernung dieser Halogenverbindungen geschieht hier durch ein separates Eindampfen der Säure im Vakuum.Chemical Abstracts 89: 30195x describes a process for cleaning gases containing sulfur dioxide, which also contain halogen compounds as constituents. These halogen compounds are removed here by separate evaporation of the acid in vacuo.

Das Ziel der vorliegenden Erfindung ist es, ein wirtschaftliches, apparativ einfaches und betriebssicheres Verfahren zur Entschwefelung von Rauchgasen zur Verfügung zu stellen, das die Nachteile der bekannten Verfahren nicht aufweist.The aim of the present invention is to provide an economical, simple apparatus and reliable method for desulfurization of flue gases which does not have the disadvantages of the known methods.

Dieses Ziel wird erreicht durch ein Verfahren, bei dem das aus dem Kraftwerk abgegebene SOZ- haltige Rauchgas vor der Oxidation am Aktivkohlekontakt einer Wäsche (1) mit einer 50- bis 85%igen Schwefelsäure und einer Wäsche (11) mit einer 5- bis 25%igen Schwefelsäure unterworfen wird.This goal is achieved by a process in which the SO Z -containing flue gas emitted from the power plant before the oxidation at the activated carbon contact of a laundry (1) with a 50-85% sulfuric acid and a laundry (11) with a 5- to Is subjected to 25% sulfuric acid.

Gegenstand der vorliegenden Erfindung ist somit ein Verfahren zur Entschwefelung SOZ- und halogenwasserstoffhaltiger Rauchgase durch katalytische Oxidation des Schwefeldioxids an feuchter Aktivkohle bei Temperaturen von 45 bis 70°C unter Bildung von 3- bis 20%iger verdünnter Schwefelsäure, welches dadurch gekennzeichnet ist, dass die verdünnte Schwefelsäure durch Kontakt mit den heissen zu entschwefelnden Rauchgasen zweistufig in Gleich- oder Gegenstromwärmeaustauschern auf eine Schwefelsäurekonzentration von 60 bis 85% eingedampft wird und in der verdünnten Schwefelsäure gelöste Chlor- und Fluorwasserstoffe durch Verdampfung aus einem Gemisch der verdünnten Schwefelsäure aus der zweiten Stufe des Wäschers mit der konzentrierten Schwefelsäure aus der ersten Stufe des Wäschers erfolgt, wobei das Gemisch eine H2S04-Konzentration von 40 bis 70% aufweist.The present invention thus relates to a process for the desulfurization of SO Z and hydrogen halide flue gases by catalytic oxidation of the sulfur dioxide on moist activated carbon at temperatures from 45 to 70 ° C. with the formation of 3 to 20% dilute sulfuric acid, which is characterized in that the diluted sulfuric acid is evaporated by contact with the hot flue gases to be desulfurized in two stages in cocurrent or countercurrent heat exchangers to a sulfuric acid concentration of 60 to 85% and in the dilute sulfuric acid dissolved hydrochloric and hydrofluoric acids by evaporation from a mixture of the dilute sulfuric acid from the second stage Washer with the concentrated sulfuric acid from the first stage of the washer, the mixture having an H 2 S0 4 concentration of 40 to 70%.

Besonders vorteilhaft ist die Ausführungsform des erfindungsgemässen Verfahrens, bei der die zu entschwefelnden Rauchgase eine Temperatur von mindestens 120°C aufweisen.The embodiment of the method according to the invention in which the flue gases to be desulfurized have a temperature of at least 120 ° C. is particularly advantageous.

Gleichzeitig mit der Erhöhung der Schwefelkonzentration auf 60 bis 85% erfolgt dabei eine Abkühlung der Rauchgase auf 90 bis 110°C.Simultaneously with the increase in the sulfur concentration to 60 to 85%, the flue gases are cooled down to 90 to 110 ° C.

Anschliessend wird eine zweite Wäsche (11) mit 5- bis 25%iger Schwefelsäure durchgeführt, bei der eine Absorption von HCI und HF in der Säure erfolgt. Dadurch werden negative Einflüsse auf die katalytische Umsetzung des S02 an der Aktivkohle vermieden. Das etwa 45 bis 70°C heisse, weitgehend von Staub befreite Rauchgas wird durch eine Aktivkohleschicht geleitet, die kontinuierlich oder diskontinuierlich mit so viel Wasser besprüht wird, dass eine 3- bis 20%ige Schwefelsäure abfliesst. Der Gasstrom kann alternativ von unten nach oben oder umgekehrt durch die Kohleschicht geleitet werden.A second wash (11) is then carried out with 5 to 25% sulfuric acid, in which the HCI and HF are absorbed in the acid. This avoids negative influences on the catalytic conversion of S0 2 on the activated carbon. The approximately 45 to 70 ° C hot, largely dust-free flue gas is passed through an activated carbon layer, which is continuously or intermittently sprayed with so much water that a 3 to 20% sulfuric acid flows off. The gas stream can alternatively be passed through the coal layer from bottom to top or vice versa.

Beim Durchströmen der Aktivkohleschicht wird das Rauchgas mit Wasserdampf gesättigt und auf 45 bis 55°C abgekühlt. Diese Abkühlung kann vermieden werden, wenn in das Rauchgas vor dem Eintritt in die Aktivkohleschicht, vorzugsweise nach Wäsche (1), Wasserdampf eingeleitet wird, z.B. bei verschiedenen Prozessen als Abdampf anfällt.When flowing through the activated carbon layer, the flue gas is saturated with water vapor and cooled to 45 to 55 ° C. This cooling can be avoided if water vapor is introduced into the flue gas before entering the activated carbon layer, preferably after washing (1), e.g. evaporation occurs in various processes.

Die im Aktivkohlereaktor bei der Entschwefelung anfallende 3- bis 20%ige Schwefelsäure ist nahezu wertlos. Erfindungsgemäss wird diese Säure über den Schwefelsäurekreislauf der Wäsche (11) letztendlich in den Schwefelsäurekreislauf der Wäsche (I) eingespeist, in dem so viel Wasser durch Verdunstungskühlung an das Rauchgas abgegeben wird, dass eine 60- bis 85%ige Schwefelsäure ausgespeist wird. Diese Säure kann entweder direkt eingesetzt werden, z.B. in der Düngemittelindustrie, oder mit relativ geringem Aufwand nach bekannten Verfahren auf einen H2S04-Gehalt von 80 bis 93% eingedampft werden.The 3 to 20% sulfuric acid obtained in the activated carbon reactor during desulfurization is almost worthless. According to the invention, this acid is ultimately fed via the sulfuric acid cycle of the laundry (11) into the sulfuric acid cycle of the laundry (I), in which so much water is released to the flue gas by evaporative cooling that a 60 to 85% strength sulfuric acid is fed out. This acid can either be used directly, for example in the fertilizer industry, or can be evaporated to an H 2 S0 4 content of 80 to 93% using known methods with relatively little effort.

Aufgrund der geringen Löslichkeit von HCI und HF in der 50- bis 85%igen Schwefelsäure bei 90 bis 110°C, würden sich diese im Rauchgas in geringen Mengen enthaltenen Verbindungen in dem zur Aktivkohle gelangenden Rauchgas immer weiter anreichern und zu einer Vergiftung des Aktivkohlekatalysators führen, wenn das Rauchgas nach der Wäsche (I) direkt in den Aktivkohlereaktor und die HCI- und HF-haltige Säure aus dem Reaktor direkt in die Wäsche (I) geleitet würde. Dies wird durch die zweite Wäsche (11) der Rauchgase mit 5- bis 25%iger Schwefelsäure bei 50 bis 70°C vermieden. Der Vorteil dabei ist, dass HCI und HF durch Adsorption in der 5- bis 25%igen Schwefelsäure weitgehend aus dem Rauchgas entfernt werden, bevor dieses in den Aktivkohlereaktor eingeleitet wird, und dass die bei der Abkühlung des Rauchgases von 90 bis 110°C auf 45 bis 70°C frei werdende Gaswärme zur Säureeindampfung genutzt wird.Due to the low solubility of HCI and HF in 50 to 85% sulfuric acid at 90 to 110 ° C, these compounds contained in small amounts in the flue gas would always turn white in the flue gas reaching the activated carbon Enrich ter and lead to poisoning of the activated carbon catalyst if the flue gas after the wash (I) would be passed directly into the activated carbon reactor and the HCI and HF-containing acid from the reactor directly into the wash (I). This is avoided by the second wash (11) of the flue gases with 5 to 25% sulfuric acid at 50 to 70 ° C. The advantage here is that HCI and HF are largely removed from the flue gas by adsorption in the 5 to 25% sulfuric acid before it is introduced into the activated carbon reactor, and that when the flue gas cools from 90 to 110 ° C 45 to 70 ° C released gas heat is used for acid evaporation.

Die Austreibung des HCI und HF aus der Waschsäure des Waschkreislaufs (11) erfolgt durch Mischen der aus der Wäsche (11) ausgespeisten HCI-und HF-haltigen 5- bis 25%igen Schwefelsäure mit so viel 60- bis 85%iger Schwefelsäure aus der Wäsche (1), dass eine 40- bis 70%ige Schwefelsäure resultiert. Aus dieser Schwefelsäure werden durch Strippen mit Luft bzw. Rauchgas oder durch Evakuieren HCI, HF und ein Teil des Wassers verdampft. Die Dämpfe können durch indirekte oder direkte Kühlung kondensiert werden.The HCI and HF are expelled from the washing acid of the washing circuit (11) by mixing the HCI and HF-containing 5 to 25% sulfuric acid fed out of the washing (11) with as much 60 to 85% sulfuric acid from the Wash (1) that a 40-70% sulfuric acid results. From this sulfuric acid, HCI, HF and part of the water are evaporated by stripping with air or flue gas or by evacuation. The vapors can be condensed by indirect or direct cooling.

In einer bevorzugten Ausführung des erfindungsgemässen Verfahrens erfolgt die Entfernung von Chlor- und Fluorwasserstoff durch Vakuumverdampfung aus einem Gemisch der verdünnten Schwefelsäure aus der zweiten Stufe des Wäschers mit der konzentrierten Schwefelsäure aus der ersten Stufe des Wäschers, wobei das Gemisch eine H2S04-Konzentration von 40 bis 70% aufweist.In a preferred embodiment of the process according to the invention, the removal of hydrogen chloride and hydrogen fluoride is carried out by vacuum evaporation from a mixture of the dilute sulfuric acid from the second stage of the scrubber with the concentrated sulfuric acid from the first stage of the scrubber, the mixture having an H 2 SO 4 concentration from 40 to 70%.

Ebenso vorteilhaft kann aber auch die Ausführung sein, bei der die Entfernung von Chlor- und Fluorwasserstoff aus einem Gemisch der verdünnten Schwefelsäure aus der zweiten Stufe des Wäschers mit der konzentrierten Schwefelsäure aus der ersten Stufe des Wäschers, wobei das Gemisch eine H2SO4-Konzentration von 40 bis 70% aufweist, durch Ausblasen mit Luft oder Rauchgas und anschliessendes Auswaschen der Halogenwasserstoffe aus dem Gas mit Wasser erfolgt.However, the embodiment in which the removal of hydrogen chloride and hydrogen fluoride from a mixture of the dilute sulfuric acid from the second stage of the scrubber with the concentrated sulfuric acid from the first stage of the scrubber can be just as advantageous, the mixture being an H 2 SO 4 - Has a concentration of 40 to 70%, by blowing out with air or flue gas and then washing out the hydrogen halide from the gas with water.

Die Kondensierung der Dämpfe kann vorteilhaft durch direkte Kühlung und Wäsche mit Kühlwasser erreicht werden.The condensation of the vapors can advantageously be achieved by direct cooling and washing with cooling water.

Das erfindungsgemässe Verfahren soll anhand von Fig. 1 verdeutlicht werden. Hier wird eine Rauchgasentschwefelungsanlage dargestellt für die Gesamtstromentschwefelung mit einem Reingas-S02-Gehalt unter 400 mg/m n, bestehend aus einer Gaswäsche (I), in der gleichzeitig eine Rauchgaskühlung und -befeuchtung, Feinstaubentfernung und Schwefelsäurekonzentrierung erfolgt, einer Gaswäsche (11), in der die weitere Gaskühlung bei gleichzeitiger Schwefelsäurekonzentrierung sowie die Feinstaubentfernung und die HCI- und HF-Entfernung aus dem Rauchgas erfolgt, einem Aktivkohlereaktor (5) zur katalytischen Umsetzung des Schwefeldioxides mit Sauerstoff und Wasser zu Schwefelsäure und einer Nebenanlage (7, 8) zur Entfernung von HCI und HF aus der Schwefelsäure. Das Rauchgas (10) wird mittels des Gebläses (9) durch den Wäscher (1) gefördert, in dem es durch den Kontakt mit 50- bis 85%iger Schwefelsäure auf 90 bis 110°C gekühlt wird.The method according to the invention will be illustrated with reference to FIG. 1. A flue gas desulfurization system is shown here for total current desulfurization with a clean gas S0 2 content below 400 mg / m n , consisting of a gas scrubber (I), in which flue gas cooling and humidification, fine dust removal and sulfuric acid concentration takes place, gas scrubbing (11) , in which the further gas cooling with simultaneous sulfuric acid concentration as well as the fine dust removal and the HCI and HF removal from the flue gas takes place, an activated carbon reactor (5) for the catalytic conversion of the sulfur dioxide with oxygen and water to sulfuric acid and an auxiliary system (7, 8) Removal of HCI and HF from sulfuric acid. The flue gas (10) is conveyed through the scrubber (1) by means of the fan (9), in which it is cooled to 90 to 110 ° C. by contact with 50 to 85% sulfuric acid.

Das aus dem Wäscher (1) austretende Gas (11) wird im Wäscher (3) mit 5- bis 25%iger Schwefelsäure kontaktiert. Dabei erfolgen eine Abkühlung des Gases auf 50 bis 70°C und die Adsorption des überwiegenden Teils des HCI und der HF in der Schwefelsäure. Das nahezu wasserdampfgesättigte und weitgehend staubfreie Rauchgas (12) wird im Reaktor (5) durch eine feuchte Aktivkohleschicht (6) geleitet, in der aus Schwefeldioxid, Sauerstoff und Wasser Schwefelsäure gebildet wird.The gas (11) emerging from the scrubber (1) is contacted in the scrubber (3) with 5 to 25% sulfuric acid. The gas is cooled to 50 to 70 ° C and the majority of the HCI and HF are adsorbed in the sulfuric acid. The almost water vapor-saturated and largely dust-free flue gas (12) is passed in the reactor (5) through a moist activated carbon layer (6), in which sulfuric acid is formed from sulfur dioxide, oxygen and water.

Das aus dem Reaktor (5) austretende Reingas (13) wird direkt oder nach Aufheizen mittels heisser Rauchgase oder eines Teilstromes des Rohgases oder nach indirekter Erwärmung in Wärmetauschern in die Atmosphäre geleitet.The clean gas (13) emerging from the reactor (5) is passed into the atmosphere directly or after heating by means of hot flue gases or a partial flow of the raw gas or after indirect heating in heat exchangers.

Die in der Aktivkohleschicht (6) des Reaktors (5) gebildete Schwefelsäure wird durch kontinuierliches oder diskontinuierliches Besprühen der Kohleschicht (6) mit Wasser (27) als 3- bis 20%ige Schwefelsäure (14) entfernt und in die Kreislaufsäure (15) der Wäsche (11) eingespeist. In der Wäsche (11) wird aus dem Sumpf des Wäschers (3) 5- bis 25%ige Schwefelsäure (15) mittels der Pumpe (4) abgezogen und im wesentlichen (16) in den Kopfteil des Wäschers gefördert. Ein Teilstrom (17), der dem Strom (14) abzüglich der im Wäscher (3) verdampften Wassermenge entspricht, wird zusammen mit 60- bis 85%iger Schwefelsäure (18) als 40- bis 70%ige Schwefelsäure (19) in einen Vakuumkühler (7) eingespeist. In diesem verdampfen HCI, HF und eine geringe Wassermenge. Die Dämpfe (21) werden in einem Einspritzkondensator (8) mit Kühlwasser (22) kondensiert und als schwach saures Abwasser (23) abgeleitet, Die HCl- und HF-freie Schwefelsäure (20) wird in den Säurekreislauf der Wäsche (I) eingespeist. In dieser Wäsche wird das Rohgas mit 60- bis 85%iger Schwefelsäure (25) gewaschen. Nach Verdampfung eines Teils des Wassers aus der Säure wird die 60- bis 85%ige Schwefelsäure (24) mittels der Kreislaufpumpe (2) aus dem Sumpf des Wäschers (1) abgezogen. Die als Produktion anfallende 60- bis 85%ige Schwefelsäure (26) kann von 90 bis 110°C durch indirekte Kühlung gekühlt oder einer weiteren Eindampfung zugeführt werden.The sulfuric acid formed in the activated carbon layer (6) of the reactor (5) is removed by continuously or discontinuously spraying the carbon layer (6) with water (27) as 3 to 20% sulfuric acid (14) and into the circulating acid (15) Laundry (11) fed. In the laundry (11), 5 to 25% strength sulfuric acid (15) is drawn off from the bottom of the washer (3) by means of the pump (4) and essentially (16) conveyed into the head part of the washer. A partial flow (17), which corresponds to the flow (14) minus the amount of water evaporated in the scrubber (3), is placed in a vacuum cooler together with 60- to 85% sulfuric acid (18) as 40-70% sulfuric acid (19) (7) fed. HCI, HF and a small amount of water evaporate in it. The vapors (21) are condensed in an injection condenser (8) with cooling water (22) and discharged as weakly acidic waste water (23). The HCl - and HF-free sulfuric acid (20) is fed into the acid cycle of the laundry (I). In this wash, the raw gas is washed with 60 to 85% sulfuric acid (25). After evaporation of part of the water from the acid, the 60 to 85% strength sulfuric acid (24) is drawn off from the bottom of the scrubber (1) by means of the circulation pump (2). The 60 to 85% sulfuric acid (26) obtained as production can be cooled from 90 to 110 ° C by indirect cooling or fed to a further evaporation.

Die Gaswäsche und die Säureeindampfung können alternativ zu den dargestellten Strahlwäschern auch in Waschtürmen, Venturiwäschern oder ähnlich geeigneten Apparaten im Gleichstrom oder Gegenstrom des Rauchgases zur eingespeisten Schwefelsäure geschehen. Ebenso kann die HCI und HF-Entfernung statt im Vakuumkühler (7) durch Ausblasen der Säure (19) mit Luft oder Rauchgas erfolgen.As an alternative to the jet scrubbers shown, the gas scrubbing and the acid evaporation can also take place in washing towers, venturi scrubbers or similarly suitable apparatuses in cocurrent or countercurrent to the flue gas to the sulfuric acid fed in. HCI and HF removal can also be carried out by blowing out the acid (19) with air or flue gas instead of in a vacuum cooler (7).

Dabei muss die HCI- und HF-beladene Luft oder das Rauchgas anschliessend mit Wasser in einem Gaswäscher gereinigt werden. Sofern eine Verwendungsmöglichkeit für die Säuren aus den Brüden (21) besteht, wird eine indirekte Kühlung dieser Brüden vorgenommen.The HCI and HF-laden air or the flue gas must then be cleaned with water in a gas scrubber. If a possible use for the acids from the broth (21), these vapors are cooled indirectly.

Im folgenden wird das erfindungsgemässe Verfahren beispielhaft erläutert, ohne dass hierin eine Einschränkung der Erfindung zu sehen ist.The method according to the invention is explained below by way of example, without any restriction of the invention being seen here.

Beispielexample

Das Beispiel betrifft eine Rauchgasentschwefelung entsprechend Fig. 1.210.000 m3 n/h Rauchgas (10) mit einem Gehalt von 7,15 Vol.-% H20, 6 Vol.- % O2. 3,3 SO2/m3 n, 0,2 g HCl/m3 n und 30 mg Staub/m3 n werden mit einer Temperatur von 130°C in den Wäscher (1) eingeleitet. Beim Kontakt mit 69%iger Schwefelsäure (25) werderr 3,06t H20/h aus dieser Säure verdampft. Aus dem Wäscher (1) gelangt das Rauchgas (11) mit 100°C in den Wäscher (3), in dem es mit 18,9%iger Schwefelsäure (16) gewaschen wird. Das mit 53°C aus dem Wäscher (3) austretende Rauchgas (12) enthält 11,75 Vol.-% H20, 3,3g SO2/m3 n, weniger als 10 mg Staub/m3 n und Spuren von HCI. Beim Durchströmen des Aktivkohlefestbettes (6) im Reaktor (5) wird der S02-Gehalt des Rauchgases durch katalytische Oxidation zu Schwefelsäure von 3,3 g/m 3 n auf 350 bis 400 mg/m3 im Reingas (13) verringert.The example relates to a flue gas desulfurization according to FIG. 1,210,000 m 3 n / h flue gas (10) with a content of 7.15% by volume H 2 0.6% by volume O 2 . 3.3 SO 2 / m 3 n , 0.2 g HCl / m 3 n and 30 mg dust / m 3 n are introduced into the scrubber (1) at a temperature of 130 ° C. Upon contact with 69% sulfuric acid (25) 3.06t H 2 0 / h is evaporated from this acid. From the scrubber (1), the flue gas (11) reaches the scrubber (3) at 100 ° C., where it is washed with 18.9% sulfuric acid (16). The flue gas (12) emerging from the scrubber (3) at 53 ° C. contains 11.75% by volume H 2 O, 3.3 g SO 2 / m 3 n , less than 10 mg dust / m 3 n and traces of HCI. When flowing through the activated carbon fixed bed (6) in the reactor (5), the S0 2 content of the flue gas is reduced by catalytic oxidation to sulfuric acid from 3.3 g / m 3 n to 350 to 400 mg / m3 in the clean gas (13).

Im Reaktor (5) wird die gebildete Schwefelsäure durch periodisches Bedüsen der Kohleschicht mit 9,75 m3/h Wasser (27) als 8,4%ige Schwefelsäure (14) ausgewaschen. Diese Schwefelsäure wird dem Säurekreislauf des Wäschers (3) zugespeist. Im Wäscher (3) werden 5,75t H20/h aus der Schwefelsäure verdampft. 4,63t/h der 18,9%igen Kreislaufsäure (17), die ausserdem 0,84% HCl enthalten, werden mit 7,15t/h 70%iger Schwefelsäure (18) aus Wäscher (1) gemischt und in den Vakuumkühler (7) als 50%ige Schwefelsäure mit 80°C (19) eingespeist. Bei 50 mbar verdampfen unter Abkühlung auf 55°C 39kg HCI/h und 283kg H20/h (21), die im Kondensator (8) durch direkten Kontakt mit 18 m3/h Kühlwasser (22) kondensiert werden. Aus dem Kondensator (8) werden die nicht kondensierbaren Gase mittels Vakuumpumpe abgesaugt.The sulfuric acid formed is washed out in the reactor (5) by periodically spraying the carbon layer with 9.75 m 3 / h of water (27) as 8.4% strength sulfuric acid (14). This sulfuric acid is fed to the acid circuit of the washer (3). In the washer (3), 5.75t H 2 0 / h are evaporated from the sulfuric acid. 4.63t / h of the 18.9% recycle acid (17), which also contain 0.84% HCl, are mixed with 7.15t / h 70% sulfuric acid (18) from the washer (1) and placed in the vacuum cooler ( 7) fed as 50% sulfuric acid at 80 ° C (19). At 50 mbar, 39kg HCI / h and 283kg H 2 0 / h (21) evaporate while cooling to 55 ° C, which are condensed in the condenser (8) by direct contact with 18 m 3 / h cooling water (22). The non-condensable gases are extracted from the condenser (8) by means of a vacuum pump.

Die HCI-freie 51%ige Schwefelsäure (20) aus dem Vakuumkühler (7) wird in den Säurekreislauf der Wäsche (I) eingespeist. Aus Wäscher (1) werden 1,24t/h 70%ige Schwefelsäure (26) mit 100°C als Produktion ausgespeist.The HCI-free 51% sulfuric acid (20) from the vacuum cooler (7) is fed into the acid cycle of the laundry (I). From washer (1), 1.24 t / h of 70% sulfuric acid (26) are fed out at 100 ° C. as production.

Claims (5)

1. A process for the desulfurization of smoke gases containing S02 and hydrogen halides by catalytic oxidation of the sulfur dioxide on moist active carbon at temperatures of from 45 to 70°C to form 3 to 20% dilute sulfuric acid, characterized in that the dilute sulfuric acid is concentrated by evaporation to a sulfuric acid concentration of 60 to 85% in two stages by contact with the hot smoke gases to be desulfurized in co-current or counter-current heat exchangers and hydrogen chlorides and fluorides dissolved in the dilute sulfuric acid are removed by evaporation of a mixture of the dilute sulfuric acid from the second stage of the scrubber with the concentrated sulfuric acid from the first stage of the scrubber, the mixture having an H2S04 concentration of 40 to 60%.
2. A process as claimed in claim 1, characterized in that the smoke gases to be desulfurized have a temperature of at least 120°C.
3. A process as claimed in claim 1 or 2, characterized in that evaporation is carried out by vacuum evaporation.
4. A process as claimed in claim 1 or 2, characterized in that evaporation is carried out by blowing out with air or smoke gas and subsequent washing out of the hydrogen halides from the gas with water.
5. A process as claimed in any of claims 1 to 4, characterized in that, after the first stage of the scrubber, steam is introduced into the smoke gas.
EP85111668A 1984-09-29 1985-09-16 Process for the desulphurization of fumes Expired EP0177806B1 (en)

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DE3567577D1 (en) 1989-02-23
JPS6254531B2 (en) 1987-11-16
DE3435931A1 (en) 1986-04-03
ATE40051T1 (en) 1989-02-15
CA1245831A (en) 1988-12-06
EP0177806A3 (en) 1987-10-07
JPS6186929A (en) 1986-05-02
US4670235A (en) 1987-06-02

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